System and method of controlling temperature of a medium by refrigerant vaporization

ABSTRACT

A system and method of controlling temperature of a medium by refrigerant vaporization, the system including a container, at least one a refrigerant reservoir having at least one reservoir section that includes a wall with an exterior surface structured to be thermally coupled with a volume of the medium in the container and to provide a volume of medium thermal coverage in the container, a vapor pressure apparatus to provide regulation of refrigerant vapor pressure in the at least one refrigerant reservoir, whereby the refrigerant reservoir forms a vapor space in each of the at least one reservoir section in response to receiving refrigerant and to the vapor pressure apparatus regulation of vapor pressure above the refrigerant to enable refrigerant vaporization at or near a selected temperature of the volume of medium in the container that is thermally coupled to the respective reservoir section.

BACKGROUND Technical Field

The present disclosure is directed to temperature control of a medium and, more particularly, to controlling the temperature of the medium by localized temperature control of respective localized thermal volumes that constitute the medium.

Description of the Related Art

Temperature control is a fundamental requirement for successful chemical reaction engineering. Biological cells grow and produce products at an optimum temperature; likewise chemical catalysts, separations, crystallizations, evaporations, filtrations, polymerizations, isomerizations, and other reactions have specific operating temperatures which best achieve desired results.

Traditional cooling methods do not have the capability of adapting to the time and spatially dependent heat production characteristics of chemical and biochemical reactions, particularly those with low heat outputs. Such reactions include ethanol and lactic acid fermentations, anaerobic digestions, pharmaceutical cell cultures, biodiesel esterifications, and industrial polymerizations. Although these reactions can generate substantial instantaneous heat, the overall heat generated is low, and heat production values often vary significantly in time and space.

For example, fermentation of red wine has a heat output that increases rapidly in the first few hours, peaks briefly, and then falls gradually over several days. Fermentation heat output is also directly proportional to the local concentration of metabolically digesting yeast, concentrations which can vary spatially inside a tank or vessel. This variance is caused by dependence on naturally generated CO₂ for agitation/homogenization, with CO₂ production also directly proportional to the local concentration of metabolically digesting yeast and further proportional to the overall heat output of the fermentation cycle.

Failure to control the fermentation temperature of red wine may adversely affect batch quality. Specifically, yeast may clump on floating skins, generate localized areas of high heat/accelerated metabolic activity, and die prematurely due to elevated, local temperatures. These deaths then result in an insufficient yeast population to complete the conversion of all sugar in the tank or vessel (an incomplete/failed fermentation). Furthermore, failure to control temperature during fermentation can alter the flavor of the wine, due to changes in yeast metabolic selectivity for production of volatile metabolites.

Traditional temperature control methods for fermentation utilize an external cooling jacket with a variable flow of chilled water or glycol and a temperature control element submerged in the reaction vessel. While this method can provide rapid cooling of a vessel volume, quickly offsetting the heat of reaction, unnecessary cooling may follow. For example, a temperature element may correctly interpret a local need for cooling when the majority of the reaction volume does not require it. Likewise, an element may correctly determine that cooling of the nearby reaction volume is not required, when, in fact, the reaction has exceeded the set-point temperature elsewhere in the tank or vessel.

One solution to this problem is agitation of the reaction volume. Agitation homogenizes the reaction volume and provides a more uniform concentration near the temperature element, better representative of the total vessel contents. However, many common biological reactions, like ethanol production during beer fermentation, are not artificially agitated as the yeast naturally generates CO₂, helping to homogenize the fermenting culture. Artificial agitation also risks accidental oxidation of the beer during fermentation, possibly altering the flavor profile and reducing shelf-life. The brewer thus must rely upon natural agitation, but cannot be certain that the vessel cooling system functions at optimal conditions due to lack of homogeneity in the fermenting volume.

As with wine fermentation, beer fermentation is also temperature sensitive. Generally, beer yeast can be divided into two categories: lagers and ales. Lager strains prefer temperatures between 45° F. and 55° F., while ale strains prefer fermentation temperatures between 60° F. and 70° F. Temperature control is crucial to ensure quality, particularly with regard to flavor and for consistency between fermenting batches. Temperature extremes, either above or below the desired range, risk both generation of unwanted chemical byproducts (esters, diacetyls, fusel alcohols, etc.) and thermal shock of the yeast, which can lead to cellular damage, including premature death.

Fermenters have been designed using conventional technology to utilize vacuum, water or air recirculation to cool tanks or vessels. For instance, U.S. Pat. No. 7,685,715 for methods for processing the contents of containers and tanks or vessels with a coaxial tank or vessels having an inner cylinder wrapped with spiral bands which are then covered by an outer cylinder whereby fluid is circulated between the cylinders to regulate the temperature of the inner cylinder and contents.

U.S. Patent Publication No. 20050077029 teaches heat exchanges for fermentation tanks or vessels using an outer cylinder with a concentric inner cylinder through which a liquid of a selected temperature is passed to regulate the temperature of the contents of the outer cylinder. U.S. Pat. No. 7,870,891 teaches using a jacketed fermenter using air as a cooling medium. U.S. Patent Publication No. 20080175951 teaches establishing a vacuum in the fermenter above the fermented liquid to control the vapor pressure.

BRIEF SUMMARY

The present disclosure is, in one implementation, directed to a system and method to control the temperature of a medium in a container, such as a tank or vessel.

In accordance with one implementation of the present disclosure, a system and method of controlling temperature of a medium by refrigerant vaporization is provided. the system includes a container, at least one refrigerant reservoir having at least one reservoir section that includes a wall with an exterior surface structured to be thermally coupled with a volume of the medium in the container and to provide a volume of medium thermal coverage in the container, a vapor pressure apparatus to provide regulation of refrigerant vapor pressure in the at least one refrigerant reservoir, whereby the refrigerant reservoir forms a vapor space in each of the at least one reservoir sections in response to receiving refrigerant and to the vapor pressure apparatus regulation of vapor pressure above the refrigerant to enable refrigerant vaporization at or near a selected temperature of the volume of medium in the container that is thermally coupled to the respective reservoir section.

In accordance with another aspect of the foregoing implementation, the at least one reservoir section comprises a plurality of reservoir sections that each have a respective internal reservoir space that is in fluid communication with at least one other internal reservoir space of an adjacent reservoir section, and the plurality of reservoir sections arranged in spaced relationship to adjacent reservoir sections with the respective volumes of medium thermal coverage having the respective boundaries of thermal coverage to be at least contiguous.

In accordance with another aspect of the foregoing implementation, the system further includes a refrigerant source in fluid communication with the refrigerant reservoir and the vapor pressure apparatus and configured to provide refrigerant to the refrigerant reservoir in response to a change in vapor pressure in the refrigerant reservoir as regulated by the vapor pressure apparatus.

In accordance with another aspect of the foregoing implementation, the plurality of reservoir sections are coupled together in series or in parallel or in a combination of series and parallel arrangements.

In accordance with another aspect of the foregoing implementation, each internal reservoir space is formed by at least one weir in the respective reservoir section, with the at least one weir sized and shaped to divide the reservoir section into a vapor space and a refrigerant space.

In accordance with another aspect of the foregoing, the refrigerant reservoir comprises a lattice of reservoir sections.

In accordance with another aspect of the foregoing implementation, R3 is a radius of the volume of medium thermal coverage that is determined as follows:

${R\; 3} = \sqrt{{\frac{1}{J*\pi}*\left( {{T\; 2} - {T\; 1}} \right)*\frac{1}{\frac{1}{2*\pi}*\left( {\frac{1}{H\; 1*R\; 1} + \frac{\ln\left( \frac{R\; 2}{R\; 1} \right)}{K\; 1} + \frac{1}{H\; 2*R\; 2}} \right)}} + {R\; 2^{2}}}$

where:

H1=Refrigerant heat transfer coefficient, including boundary layer effects (W/m²*K);

H2=Medium heat transfer coefficient, including boundary layer effects (W/m²*K);

J=Heat generated by medium per unit volume per unit time (W/m³);

K1=Thermal conductivity of refrigerant reservoir wall material of construction (W/m*K);

R1=Radius from center of reservoir section to interior of reservoir section wall (m);

R2=Radius from center of reservoir section to exterior of reservoir section wall (m);

R3=Radius from center of reservoir section to outside boundary of liquid medium thermal coverage (m);

T1=Temperature of refrigerant at a location of vaporization (K); and

T2=Temperature of the medium at an outer boundary of thermal coverage (K).

In accordance with another aspect of the foregoing implementation, a minimum spacing between a center of adjacent reservoir sections is not less than

$\frac{2}{\sqrt{2}}*R\; 3$ and R3 is a radius of the volume of medium thermal coverage.

In accordance with still yet another aspect of the present disclosure, the at least one refrigerant reservoir is located in the interior of the container or, alternatively, the at least one refrigerant reservoir is located on the exterior of the container, or the at least one refrigerant reservoir includes at least two refrigerant reservoirs, with at least one refrigerant reservoir located in the interior of the container and at least one refrigerant reservoir located on the exterior of the container.

In accordance with another implementation of the present disclosure, a method of controlling the temperature of a medium by refrigerant vaporization is provided, the method including:

providing an apparatus for controlling the temperature of a medium by refrigerant vaporization of a refrigerant, the providing including providing:

-   -   a container having an exterior and an interior;     -   at least one refrigerant reservoir associated with the         container, the at least one refrigerant reservoir having at         least one reservoir section configured to hold refrigerant, each         at least one reservoir section having a wall with an exterior         surface structured to be thermally coupled with a volume of the         medium in the container and to provide thermal change to the         volume of the medium in the container and thereby provide a         volume of medium thermal coverage in the container, the volume         of medium thermal coverage having an outside boundary;     -   a vapor pressure apparatus to provide regulation of refrigerant         vapor pressure in the at least one refrigerant reservoir; and     -   wherein the at least one refrigerant reservoir is configured to         form a vapor space in each of the at least one reservoir         sections in response to receiving refrigerant and in response to         the vapor pressure apparatus regulation of vapor pressure above         the refrigerant to enable refrigerant vaporization at or near a         selected temperature of the volume of medium thermal coverage         for the volume of the medium in the container that is thermally         coupled to the respective at least one reservoir section;

introducing refrigerant into the at least one refrigerant reservoir to partially occupy the at least one refrigerant section and form a vapor space in the at least one refrigerant section; and

regulating vapor pressure above the refrigerant in the at least one refrigerant reservoir to enable refrigerant vaporization at or near a selected temperature of the volume of medium thermal coverage for the volume of the medium in the container that is thermally coupled to the respective at least one reservoir section.

In accordance with another aspect of the present disclosure, a method of controlling temperature in a medium stored in a container is provided. The method includes the steps of partitioning the medium into localized thermal volumes, and thermally coupling a refrigerant to respective localized thermal volumes to control the temperature of the localized thermal volume to maintain the medium at a selected temperature.

In accordance with a further aspect of the foregoing method, partitioning the medium into localized thermal volumes includes positioning a refrigerant reservoir in physical proximity to the container, with at least one refrigerant reservoir section associated with a respective localized thermal volume.

In accordance with still yet another aspect of the foregoing method, the thermally coupling includes regulating vapor pressure in a vapor space above the refrigerant in each at least one refrigerant reservoir section to maintain a temperature of the respective localized thermal volume at the selected temperature of the medium.

As will be readily appreciated from the foregoing, the present disclosure provides a system and method for controlling the temperature of a medium by providing localized temperature control of the medium. While representative implementations of the present disclosure are described in the context of fermentation, the system and method of the present disclosure will have application to both heating and cooling of a medium in order to maintain temperature in a wide variety of mediums, and is a novel approach to engineered temperature control that adjusts to both time and spatial variances in heat production without the need for advanced controls and programming. As opposed to traditional methods, which cool the entire system volume with maximum intensity but for varying lengths of time, the novel approach of the present disclosure adjusts temperature of only those spatial areas that, for example, generate heat and with an intensity directly proportional to local heat production. Heating of the medium, then, is not accomplished directly, but rather through careful regulation of the net heat output of a reaction. The refrigerant vapor pressure can be modulated to increase the set-point temperature of medium and the present disclosure ensures that the allowable local increases in temperature never exceed that new set-point. Thus slow, deliberate heating of the medium can be affected.

Traditional systems employ chilled water or glycol that activate whenever a measured set-point temperature has been exceeded. Activation is controlled by the local temperature near the sensing element and cooling is accomplished rapidly through the use of large temperature gradients between the water or glycol and system volume. Once a lower temperature set-point has been achieved, the cooling system is then deactivated.

This approach has two distinct disadvantages: 1. the entire system volume is cooled based upon a local subset of conditions, and 2. the entire system volume is subjected to large temperature gradients for the duration of the cooling cycle. Thus, the system contents located at a distance from the sensing element are cooled regardless of need, and system contents can be subject to thermal cold shock. This cold shock may be more pronounced for contents located near an external cooling jacket or internal cooling coil, particularly when the system volume lacks consistent agitation or homogenization.

The present disclosure avoids these disadvantages by using a refrigerant located in shallow, horizontal liquid tubes, and connected by a common vapor headspace. The refrigerant is held at or close to the desired temperature of the system volume and its vapor pressure is controlled such that the refrigerant vaporizes at this same temperature. Because the liquid in the horizontal tubes is not hydraulically connected, each horizontal section then vaporizes at approximately the same pressure/temperature as the horizontal sections above and below.

Temperature control of the system volume is affected by control of the vapor pressure of the refrigerant. The refrigerant, when at its vaporization point, requires large energy uptake to change phases, but will absorb this energy at constant temperature until the refrigerant mass is depleted. Thus any local system volume near the horizontal tubes is protected from exceeding the vaporization temperature of the refrigerant therein, as long as those tubes contain refrigerant.

The present disclosure provides passive, continual, and continuous protection against an increase in system volume, set-point temperature. A temperature sensing element is no longer required to activate the cooling system, as local refrigerant vaporization removes heat as soon as it is generated and near its spatial point of generation. Additionally, a high temperature gradient for cooling is not required, as heat transfer must no longer be accomplished rapidly and across large distances (e.g., container wall to container center). As local heat generation varies, the local temperature differential between the system volume and refrigerant coil also varies, and heat will be removed proportionally by a waiting mass of local refrigerant.

In summary, the systems and methods of the present disclosure improve significantly on traditional temperature control methods. The approach no longer risks unnecessarily cooling the entire system volume based upon conditions near a local, temperature sensing element or failing to activate that cooling system, when needed, based upon local conditions near the sensing element. The present disclosure also avoids the need to create large temperature gradients that may risk thermal cold shock of system contents. Furthermore, controlled heating of the medium can be affected using the system's own exothermic heat without risk of overshoot and the possibility of thermal hot shock of system contents. Benefits of improved temperature control include optimized reaction rates, reduced undesirable side-reactions, and improved consistency between batches for batch processes.

BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS

The foregoing and other features and advantages of the present disclosure will be more readily appreciated as the same become better understood from the following detailed description when taken in conjunction with the accompanying drawings, wherein:

FIG. 1 is an illustration of radial heat transfer along a length of horizontal lattice section in accordance with the present disclosure;

FIG. 2 is a cross section illustration of radial heat transfer along the length of horizontal lattice section of FIG. 1 ;

FIG. 3 is an illustration of the derivation of ideal spacing between lattice tubes calculated via right-angle geometry in accordance with the present disclosure;

FIG. 4 is a cross section illustration of multiple cooling volumes with minimal coverage in accordance with the present disclosure;

FIG. 5 is a cross section illustration of multiple cooling volumes with partial coverage in accordance with the present disclosure;

FIG. 6 is a cross section illustration of multiple cooling volumes with complete coverage in accordance with the present disclosure;

FIG. 7 is an illustration of a system formed in accordance with a representative implementation of the present disclosure;

FIG. 8 is a cross section side elevation of a refrigerant reservoir formed in accordance with the present disclosure and positioned in the interior of a container;

FIG. 9 is a top plan view of the refrigerant reservoir of FIG. 8 ;

FIG. 10 is an illustration of a refrigerant reservoir on the exterior of a container in accordance with another implementation of the present disclosure;

FIG. 11 is an illustration of a system formed in accordance with a representative implementation of the present disclosure in which pressure control by zones is effected by multiple pressure regulators;

FIG. 12 is a pictorial representation of an alternative implementation of the present disclosure in which the coil apparatus is exterior to the container;

FIG. 13 is an illustration of an oscillatory vacuum coil and reservoir design in which fluid in the coils will oscillate due to pressure differentials in accordance with another implementation of the present disclosure;

FIG. 14 is a side elevation cross-section illustration of a refrigerant reservoir formed in accordance with an alternative implementation of the apparatus of FIG. 8 ; and

FIG. 15 is a side elevation in cross section illustrating a refrigerant reservoir formed in accordance with another alternative implementation of the apparatus of FIG. 8 .

DETAILED DESCRIPTION

In the following description, certain specific details are set forth in order to provide a thorough understanding of various disclosed implementations. However, one skilled in the relevant art will recognize that implementations may be practiced without one or more of these specific details, or with other methods, components, materials, etc. In other instances, well-known structures associated with tanks or vessels, refrigerant, vaporization systems and vacuum systems, tubing, pipes, and coils have not been shown or described in detail to avoid unnecessarily obscuring descriptions of the implementations. Reference to “medium” is intended to include gas, liquid, solid, as well as gel and other states. Reference to “container” is intended to include, without limitation, tanks and vessels. In addition, reference to “pipe” or “tube” is intended to encompass conduits of various cross-sectional geometric configurations and conduits of any length unless otherwise specified herein.

Unless the context requires otherwise, throughout the specification and claims which follow, the word “comprise” and variations thereof, such as, “comprises” and “comprising” are to be construed in an open, inclusive sense, that is as “including, but not limited to.”

Reference throughout this specification to “one implementation” or “an implementation” means that a particular feature, structure or characteristic described in connection with the implementation is included in at least one implementation. Thus, the appearance of the phrases “in one implementation” or “in an implementation” in various places throughout this specification are not necessarily all referring to the same implementation. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more implementations. It will be appreciated that for simplicity and clarity of illustration, where considered appropriate, reference numerals may be repeated among the figures to indicate corresponding or analogous elements or steps.

As used in this specification and the appended claims, the singular forms “a,” “an,” and “the” include plural referents unless the content clearly dictates otherwise. It should also be noted that the term “or” is generally employed in its broadest sense, that is as meaning “and/or” unless the content clearly dictates otherwise.

The headings and Abstract of the Disclosure provided herein are for convenience only and do not interpret the scope or meaning of the implementations.

In contrast to traditional refrigeration methods, the present disclosure provides for process cooling of a medium utilizing a minimum temperature gradient. While a gradient must be generated to transfer heat successfully in accordance with the present disclosure, this gradient does not need to be large due to the low heat output from many common processes (for example, cell cultures) and if the heat can be removed as it is generated. Moreover, large temperature gradients between a cooling source and a target volume (i.e., medium) may actually damage the medium via thermal cold shock near the cooling system interface. This can occur, for example, near the interior wall of jacketed, cell culture reactors.

Generally, the mechanical structure of some of the implementations of the present disclosure resembles a metal lattice work. In one aspect of the present disclosure, this structure is immersed in the volume requiring temperature control. Alternatively, this lattice work can be exterior to the container holding the medium. Ideally, lattice geometry, materials of construction and refrigeration system components are determined as a function of the medium to be cooled. However, with a given lattice geometry, material of construction, and refrigeration system, cooling performance of structures formed in accordance with the present disclosure can be determined for any medium.

It is to be understood that while representative implementations of the present disclosure will be discussed in the context of cooling a medium, such as in the process of beer and wine fermentation, the systems and methods of the present disclosure will have application in other processes and in heating as well as cooling of various media.

The design of a lattice in accordance with the present disclosure has three primary aspects: (1) lattice internal dimensions, (2) lattice material of construction, and (3) spacing between adjacent lattice parts. All lattice designs have a common headspace and horizontally isolated sections holding volumes of liquid refrigerant. These characteristics ensure that refrigerant in each horizontal section evaporates at the same temperature and that there is always sufficient liquid refrigerant present to evaporate the heat generated nearby. Maintenance of liquid refrigerant height in each horizontal section is often a function of the orientation of that section with respect to gravity.

Theoretically, a lattice may be comprised of a series of horizontal sections of any shape and size, so long as those sections can store liquid refrigerant. Practically, it is most cost-effective to use a cylindrical pipe or tubing, by definition rated for the full vacuum conditions required of many refrigerants, instead of resorting to the advanced fabrication techniques required for odd-shaped, full-vacuum rated vessels. Also, it is ideal to maintain this pipe at a maximum of 70% full in order to provide sufficient surface area for liquid refrigerant vaporization from the interior surface of the headspace while still holding maximum liquid refrigerant volume inside the pipe/tubing. Additionally, free headspace allows unobstructed movement of the evaporated vapor along the length of the horizontal section to the vacuum source. The choice of lattice internal design is application specific, however, particularly with respect to refrigerant choice and refrigeration method (vacuum pump, compressor, etc.).

Theoretically, lattice material of construction is limited by the requirement that the material be mechanically compatible with the medium to be cooled and be compatible with operating conditions of the refrigerant trapped within. Practically, the material of construction is often determined by cleaning requirements (ex. sanitary requirements for cell cultures) and by those material thicknesses commercially available. The choice of lattice material of construction is application specific, however, and the thickness of material may be adjusted to improve heat transfer, despite the increased cost, for example.

Theoretically, spacing between adjacent lattice parts is a function of the medium to be cooled and its desired temperature profile and is also independent of horizontal length. For example, flavor profiles of a certain wine may be best produced at a range of 5° F., from 70° F. to 75° F., and spacing is then configured such that the outer lattice surface is held at 70° F. with a maximum of 75° F. to occur at the centerline between adjacent spacings. Practically, spacing between lattice sections is often a function of desired material of construction, welding costs, container geometry, ease of removal for maintenance, ease of cleanability, etc. An ideal spacing can be determined, however, by applying radial heat transfer equations to a horizontal coil section neglecting the length of that section (see drawings and derivations). Horizontal length, instead, is almost always determined by the need to provide the desired lattice spacing through the medium to be cooled and to ensure the presence of sufficient liquid volume of refrigerant in each horizontal section.

Use of a mathematical approach is preferred because ideal lattice spacing can be determined with a series of user-defined variables. A further advantage is that a complete lattice structure can be designed by examining the spacing requirements for a cross section of a single, horizontal lattice element.

If, for example, sanitary requirements require a specific material of construction, and the choice of refrigeration system require a certain refrigerant, both of these criteria can be incorporated into the spacing equation. Likewise, for an existing lattice structure and refrigeration system, the expected temperature gradient inside the medium to be cooled can be calculated for any medium type.

An important user-defined temperature variable is the maximum allowable temperature difference inside the medium to be cooled. For example, if a maximum temperature gradient of 5° F. and a maximum temperature of 75° F. is desired, ideal lattice spacing can be calculated using the derived equations described in more detail below, assuming a refrigerant vaporization temperature of 70° F. inside the lattice pipe and a centerline temperature of 75° F. in the medium between adjacent lattices.

The 5° F. value described is actually larger than the minimum temperature gradient required for successful heat transfer, however. In reality, this value is the total driving force required to drive heat from the furthest extent of medium to the location of refrigerant vaporization, a greater value than that required to drive heat only to the outer surface of the lattice.

This larger value actually has three components: (1) the temperature difference to transfer heat from the centerline between lattices, through the medium to be cooled, and to the surface of the lattice; (2) the temperature difference to transfer heat from the exterior surface of the lattice, through the lattice mechanical structure, and to its interior surface; and (3) the temperature difference to transfer heat from the interior surface of the lattice, through the liquid refrigerant, and to the liquid-vapor refrigerant interface where evaporation will occur.

More particularly, for heat transfer through a target medium, the maximum allowable temperature gradient is determined by the end-user. This value varies based upon the desired properties of the medium over the time-scale of cooling (ex. flavor profile). For a different medium and a fixed lattice spacing, the larger the gradient value, the greater that medium's resistance to heat flow. An increase in effective surface area for heat transfer from the medium to the lattice may reduce this gradient, however. Additional surface area may be created through the use of fin-type structures, attached to the outer surface of the lattice, for example.

The temperature gradient across the wall of the lattice mechanical structure is a function of the lattice material of construction and of its thickness. For a common lattice geometry and construction, this gradient value is constant, regardless of the medium to be cooled.

The temperature gradient from the interior wall of the lattice to the liquid-vapor refrigerant interface is a function of the chosen refrigerant and of the distance from the interior wall to the interface. For a known refrigerant and liquid refrigerant height inside the tube, this gradient value is constant, regardless of the medium to be cooled. Moreover, the headspace of a partially-filled liquid refrigerant tube may form a thin liquid film of evaporating refrigerant on its interior surface, reducing the distance required for heat to travel from a percentage of the interior surface to the liquid-vapor interface. Purposeful roughing of the interior surface may also improve vaporization heat transfer, effectively reducing the temperature gradient required to drive an equivalent amount of heat from the interior wall to the liquid-vapor refrigerant interface.

For a given lattice geometry, materials of construction, and refrigeration system, a horizontal section is responsible for cooling an identical volume of medium. However, the heat generated by that volume may change as a function of the medium properties and thus the observed cooling performance of the lattice may change also.

Referring to FIGS. 1 and 2 , for a given horizontal lattice section 50, the mechanical design must be capable of removing the maximum heat generated by a medium volume 52 surrounding that horizontal lattice section 50 that has an outside boundary 53. This volume can be approximated by assuming a cylindrical shape surrounding the horizontal lattice section 50 with a radius R3, the combination of the distance from lattice centerline to the tube exterior R2 and the distance from the lattice exterior to a centerline between adjacent lattices. The volume of the mechanical lattice is then subtracted from the total volume of the medium filled container to calculate the volume of the heat producing medium.

R1 is the inner radius of a lattice tube 54 and should be selected as a function of the refrigeration system desired. In a batch-fill system, each horizontal lattice tube 54 will need to retain enough refrigerant mass to absorb the maximum heat generated by the surrounding medium for a given time between fills (e.g., 1 hour). In a constant refill refrigeration system, this volume can be much smaller but is still subject to the criteria that sufficient refrigerant volume for vaporization remains throughout the entire horizontal length during maximum medium heat production.

With a value for R1 governed primarily by choice of refrigeration system, the horizontal length L of horizontal lattice sections 50 becomes the primary variable for establishing the refrigerant hold volume. In practice, the chosen length L per horizontal lattice section 50 almost always exceeds the minimum required, as this value is chosen primarily for structural support reasons, and to ensure that the minimum spacing requirement is satisfied throughout the medium.

Lattice geometry (spacing) varies based upon several variables, including medium, refrigerant, refrigeration method, and material of construction. Ideal spacing between adjacent lattice centerlines for production of wine, for example, would be roughly 6 inches using a lattice of 1″ OD sanitary stainless tubing, ethanol refrigerant under vacuum, and with an allowable temperature variation of 5° F. A 10° F. allowable temperature variation would increase this ideal spacing to approximately 9 inches; a change from 1″ to 2″ OD tubing at the same 10° F. difference would further increase ideal spacing to roughly 12 inches.

Also, design consideration must be given to a pressure drop in a lattice headspace 56 during system operation. For example, in a batch fill system with a vacuum pump, the pressure at an interface 58 of the liquid 60 and vapor refrigerant 62 will always be greater than the pressure at a vacuum source. Maintaining this pressure drop at a minimum is an important criterion of lattice design as it reduces the vacuum level that must be maintained at the vacuum source.

To illustrate, for 700 L of fermenting wine, a maximum liquid ethanol vaporization rate of 2 L/hr can be expected. This liquid mass vaporization corresponds to approximately 5 CFM of vapor generation at an 80° F. set-point temperature. With an allowable pressure drop due to system geometry of only 5%, 0.75″ ID piping can be used to connect the headspace to the vacuum source, if the equivalent length of that piping (linear length and fittings) does not exceed approximately 115 ft.

Additionally, the lattice design and mathematical methodology can be adapted for use outside a container, in place of a cooling jacket. This might be beneficial, particularly for small diameter vessels, as the lattice would not be in contact with the end product and thus does not require cleaning between batches. However, this design may only be of practical use if the spacing between adjacent lattices is calculated near that of a container diameter.

An example of a mathematical derivation to determine ideal coil spacing is provided below:

$\begin{matrix} {V = {I*R}} & {{Electrical}\mspace{14mu}{Analogy}} \\ {{\Delta\; T} = {Q*R}} & {{Heat}\mspace{14mu}{Transfer}\mspace{14mu}{Equation}} \\ {\frac{\Delta\; T}{L} = \frac{Q*R}{L}} & {{Divide}\mspace{14mu}{by}\mspace{14mu}{Length}\mspace{14mu}{of}\mspace{14mu}{Horizontal}\mspace{14mu}{Section}} \\ {\frac{Q}{L} = \frac{\Delta\; T}{R*L}} & {Rearrange} \end{matrix}$ L=Length of horizontal lattice section (m) Q=Total heat transferred from medium to horizontal section per unit time (W) R=Total resistance to heat transfer across the temperature differential per unit time (K/W) ΔT=Maximum temperature difference between medium and evaporating refrigerant (K)

$\begin{matrix} {{\Delta\; T} = {{T\; 2} - {T\; 1}}} & \begin{matrix} {Temperature} \\ {{Differential}\mspace{14mu}(K)} \end{matrix} \\ {R = \left( {\frac{1}{H\; 1*A\; 1} + \frac{\ln\left( \frac{R\; 2}{R\; 1} \right)}{2*\pi*L*K\; 1} + \frac{1}{H\; 2*A\; 2}} \right)} & \begin{matrix} {{Resistance}\mspace{14mu}{to}\mspace{14mu}{Heat}} \\ {{Transfer}\mspace{14mu}\left( {K/W} \right)} \end{matrix} \\ \begin{matrix} {R = {\frac{1}{2*\pi*L}*}} \\ \left( {\frac{1}{H\; 1*R\; 1} + \frac{\ln\left( \frac{R\; 2}{R\; 1} \right)}{K\; 1} + \frac{1}{H\; 2*R\; 2}} \right) \end{matrix} & {Substituting} \\ \begin{matrix} {{R*L} = {\frac{1}{2*\pi}*}} \\ \left( {\frac{1}{H\; 1*R\; 1} + \frac{\ln\left( \frac{R\; 2}{R\; 1} \right)}{K\; 1} + \frac{1}{H\; 2*R\; 2}} \right) \end{matrix} & \begin{matrix} {{Resistance}\mspace{14mu}{to}\mspace{14mu}{Heat}\mspace{14mu}{Transfer}} \\ {{Across}\mspace{14mu}{Length}\mspace{14mu}\left( {K*{m/W}} \right)} \end{matrix} \\ {Q = {J*\left( {{\pi*R\; 3^{2}*L} - {\pi*R\; 2^{2}*L}} \right)}} & \begin{matrix} {{Heat}\mspace{14mu}{Generated}\mspace{14mu}{by}} \\ {{Medium}\mspace{14mu}{per}\mspace{14mu}{Unit}\mspace{14mu}{Time}} \\ {{for}\mspace{14mu} a\mspace{14mu}{Horizontal}} \\ {{Section}\mspace{14mu}(W)} \end{matrix} \\ {\frac{Q}{L} = {J*\pi*\left( {{R\; 3^{2}} - {R\; 2^{2}}} \right)}} & \begin{matrix} {{Heat}\mspace{14mu}{Generated}\mspace{14mu}{by}} \\ {{Medium}\mspace{14mu}{per}\mspace{14mu}{Length}\mspace{14mu}{of}} \\ {{Horizontal}\mspace{14mu}{Section}\mspace{14mu}{per}} \\ {{Unit}\mspace{14mu}{Time}\mspace{14mu}\left( {W/m} \right)} \end{matrix} \end{matrix}$ A2=Surface area of exterior wall of horizontal lattice section (m²) H1=Refrigerant heat transfer coefficient, including boundary layer effects (W/m²*K) H2=Medium heat transfer coefficient, including boundary layer effects (W/m²*K) J=Maximum heat generated by medium per unit volume per unit time (W/m³) K1=Thermal conductivity of lattice material of construction (W/m*K) R1=Radius from center of horizontal lattice section to inside of lattice wall (m) R2=Radius from center of horizontal lattice section to outside of lattice wall (m) R3=Radius from center of horizontal lattice section to outside of medium volume (m) T1=Temperature at liquid-vapor refrigerant interface (K) T2=Temperature of medium at outer edge of medium volume (K)

$\begin{matrix} {{{\frac{Q}{L}*\left( {R*L} \right)} - {\Delta\; T}} = 0} & \begin{matrix} {{The}\mspace{14mu}{Rearranged}\mspace{14mu}{Heat}\mspace{14mu}{Transfer}} \\ {{Equation}\mspace{14mu}{Set}\mspace{14mu}{Equal}\mspace{14mu}{to}\mspace{14mu}{Zero}} \end{matrix} \\ \begin{matrix} {J*\pi*\left( {{R\; 3^{2}} - {R\; 2^{2}}} \right)*\frac{1}{2*\pi}*} \\ {\left( {\frac{1}{H\; 1*R\; 1} + \frac{\ln\left( \frac{R\; 2}{R\; 1} \right)}{K\; 1} + \frac{1}{H\; 2*R\; 2}} \right) -} \\ {\left( {{T\; 2} - {T\; 1}} \right) = 0} \end{matrix} & {Substituting} \\ {{R\; 3} = \sqrt{\begin{matrix} {\frac{1}{J*\pi}*\left( {{T\; 2} - {T\; 1}} \right)*} \\ {\frac{1}{\frac{1}{2*\pi}*\begin{pmatrix} {\frac{1}{H\; 1*R\; 1} +} \\ {\frac{\ln\left( \frac{R\; 2}{R\; 1} \right)}{K\; 1} +} \\ \frac{1}{H\; 2*R\; 2} \end{pmatrix}} + {R\; 2^{2}}} \end{matrix}}} & {{Setting}\mspace{14mu}{Equal}\mspace{14mu}{to}\mspace{14mu} R\; 3} \end{matrix}$

This equation can be solved for value R3, given user-defined values for all other variables. User-defined values can originate from published literature, previous design experience, allowable temperature variation in the medium, commercially available pipe/tubing sizes and thicknesses, etc. Note that this mathematical analysis is independent of the length of the horizontal section.

With a known value for R3, the ideal spacing between tubes is calculated via right-angle geometry. The derivation of this equation is as shown in FIG. 3

Note that in this example, the variable R3 is equal to the sum of a+b+c, where “a” is the lattice pipe outer radius, “b” the distance between the lattice tube and a small clump of yeast cells, and “c” the radius of that clump. Total spacing between lattice tube centerlines is equal to

$\frac{2}{\sqrt{2}}*R\; 3.$ Also, this method assumes significant overlap of the radial cooling volumes between adjacent lattice sections such that that no part of the medium volume can exceed the maximum temperature differential specified.

As shown in FIGS. 4-6 , alternative geometric configurations can increase spacing between lattice sections, however, some part of the medium then may exceed the design temperature range due to insufficient cooling. FIG. 4 is a cross section illustration of multiple cooling volumes with minimal coverage, FIG. 5 is a cross section illustration of multiple cooling volumes with partial coverage, and FIG. 6 is a cross section illustration of multiple cooling volumes with complete coverage.

FIG. 7 illustrates a system 70 to control the temperature of a medium 72 by refrigerant vaporization. In this representative implementation the system includes a container 74 having an exterior 76 and an interior 77. At least one a refrigerant reservoir 78 is associated with the container 74, the refrigerant reservoir 78 includes at least one reservoir section 80 structured to hold refrigerant 82 in an internal reservoir space 83. In this implementation there are a plurality of reservoir sections 80 as shown more clearly in FIGS. 8 and 9 , each reservoir section 80 having a wall 84 with an exterior surface 86 structured to be thermally coupled with a volume of the medium in the container 74 and to provide thermal change to the volume of the medium in the container 74 and thereby provide a volume of medium thermal coverage 52 in the container as described above in connection with FIGS. 1-6 and to be described more fully below.

Each of the reservoir sections 80 has its respective internal reservoir space 83 in fluid communication with at least one other internal reservoir space 83 of an adjacent reservoir section 80, and the plurality of reservoir sections 80 are arranged in spaced relationship to adjacent reservoir sections 80 with the respective volumes of medium thermal coverage 52 having the respective boundaries of thermal coverage to be at least contiguous.

The system 70 further includes a vapor pressure apparatus 88 to provide regulation of refrigerant vapor pressure in the reservoir sections 80. The reservoir sections 80 are each configured to form a vapor space 90 in each reservoir section 80 in response to receiving refrigerant 82 and in response to the vapor pressure apparatus 88 regulation of vapor pressure above the refrigerant 82 to enable refrigerant vaporization at or near a selected temperature of the volume of medium thermal coverage 52 for the volume of the medium 72 in the container 70 that is thermally coupled to the respective reservoir section 80.

It is to be understood that the vapor pressure apparatus 88 can be implemented with readily available commercial equipment and hence will not be described in detail herein. Briefly, the vapor pressure apparatus 88 includes a vacuum pump 92 in fluid communication with the refrigerant reservoir 78. Ideally, a pressure regulator 94 is positioned between the vacuum pump 92 and the refrigerant reservoir 78. Control of the vacuum pump 92 can be performed manually or, more preferably, by automated controls that utilize sensors and a computer processor to process signals from the sensors and transmit control signals to the vacuum pump in response to the sensor signals.

In the implementation of FIG. 7 , a condenser 96 is provided to condense a refrigerant, such as ethanol. The condenser 96 is in fluid communication with the refrigerant reservoir 78 to provide either a continuous or continual supply of refrigerant to the refrigerant reservoir 78. A chilled water tank 98 is coupled to the condenser 96 via a water pump 100 for fluid communication of water.

A refrigerant source, such as a refrigerant tank 102, is in fluid communication with the refrigerant reservoir 78 and the vapor pressure apparatus 88 and is configured to provide refrigerant 82 to the refrigerant reservoir 78 in response to a change in vapor pressure in the refrigerant reservoir 78 as regulated by the vapor pressure apparatus 88. The condenser 96 is also in fluid communication with the refrigerant tank 102 via a vent solenoid 104. In turn, the refrigerant tank 102 is coupled to the refrigerant reservoir 78 to supply refrigerant to the refrigerant reservoir 78 via a refrigerant pump 106 and in parallel with a drain solenoid 108. An isolation solenoid 110 is positioned between the refrigerant reservoir 78 and the parallel connection of the refrigerant pump 106 and the drain solenoid 108. The element LT is a level transmitter that senses and transmits an indication of the volume of refrigerant in the refrigerant tank 102. The element PT is a pressure transmitter that senses and communications an indication of the vapor pressure of the refrigerant in the vapor space.

In the implementation of FIG. 7 , the refrigerant reservoir 78 is automatically refilled at regular intervals via the refrigerant pump 106 to replenish refrigerant 82 that has evaporated in order to provide temperature control of the medium 72. The vent solenoid 104 recovers refrigerant from the condenser 106 to the refrigerant tank 102. The vent solenoid 104 also provides a closed-loop path from the refrigerant pump 106 to the refrigerant tank 102 ensuring that the internal reservoir space 83 is completely filled with refrigerant 82. The drain solenoid 108 functions to remove excess refrigerant 82 from the refrigerant reservoir 78 to the refrigerant tank 102 via gravity, creating the vapor space 90.

As shown in FIG. 8 , the refrigerant reservoir 78 in one implementation has a manifold 112 coupled to each of the reservoir sections 80 to provide fluid communication to an air vent line 114 and to a combination fill, drain, and vacuum line 116, which allows for system refrigerant fill and refrigerant drain, and system connection to the vacuum pump 92. The plurality of reservoir sections 80 may be coupled together in series or in parallel or in a combination of series and parallel arrangements. The refrigerant reservoir 78 in one implementation comprises a lattice of reservoir sections 80. Each reservoir section 80 is held in place by a vertical support 93 as is the manifold 112. Each reservoir section 80 includes at least one weir 117 in the respective reservoir section, with the weir 117 sized and shaped to divide the reservoir section into the vapor space 90 and a space for refrigerant 82. In this implementation, the weir 117 is a bent section of the tube or coil that forms the reservoir section 80, and the weir 117 includes a first wall 119 that angles upward to meet a second wall 121 that angles downward and form an apex 123. The apex 123 acts as a dam for the refrigerant 82, and its height in the reservoir section 80 determines how much refrigerant 82 will be retained in that reservoir section 80.

In accordance with another aspect of the present disclosure, the refrigerant reservoir 78 may be located on the exterior of the container 74, which is shown in FIG. 10 .

In operation, refrigerant 82 is introduced into the refrigerant reservoir 78 to partially occupy the reservoir sections 80 and form a vapor space 90 above the refrigerant 82 in the internal reservoir space 83 of each reservoir section 80. The vapor pressure above the refrigerant 82 in the refrigerant reservoir 78 is regulated to enable refrigerant vaporization at or near a selected temperature of the volume of medium thermal coverage 52 for the volume of the medium 72 in the container 74 that is thermally coupled to the respective reservoir section.

System operation requires that the refrigerant vaporize at a uniform or, preferably, an identical temperature throughout the coil. Also, a liquid refrigerant volume must be maintained throughout the coil, sufficient to remove via vaporization the heat generated by the medium. Proper orientation of the coil with respect to gravity ensures that the volume of liquid refrigerant therein matches the design intent of the coil weirs and dams. The coil metallurgy must be selected so as not to adversely affect the quality of the medium to be cooled, and the coil should be cleaned between uses to avoid possible contamination of the new medium to be cooled. Refrigerant vapor pressure should provide for refrigerant vaporization at or as close as possible to the desired temperature of the medium to be cooled, so as to avoid possible thermal shock of the medium.

In a batch type system with vacuum pump, the coil must be properly oriented with respect to gravity, filled with liquid refrigerant, drained to create a common headspace connecting the horizontal sections, and isolated to allow creation of a common vapor pressure space above all remaining liquid refrigerant inside. The vacuum pump is activated and a vacuum regulator allows adjustment of the refrigerant vapor pressure to match the desired heat removal profile for a given medium. The time between liquid refrigerant refills should be kept to a maximum, as during the refill sequence, the coil is unable to provide cooling. However, the time between refills must also be frequent enough to ensure that sufficient liquid refrigerant remains present in all sections of the coil so as to provide the desired volume of medium thermal coverage. Selection of refrigerant vapor pressure and time between refills is a function of the heat production profile of the medium to be cooled with respect to time. Ideally, during refill, the temperature of fresh liquid refrigerant should be at or near the desired set-point temperature of the medium to be cooled so as to avoid thermal shock of the medium.

In a continuous style system with traditional refrigerant compressor, proper orientation of the coil with respect to gravity ensures optimal system performance, as the refrigerant liquid volumes are then maintained at design in each horizontal section. The common vapor headspace is then likewise maintained at design. Compressor performance must also be monitored relative to the heat production profile of the medium with respect to time. Most importantly, the compressor must be capable of continued operation at variable flowrates of vapor refrigerant and throughout the desired range of refrigerant vapor pressures. Cell cultures, for example, can vary in heat production rate as a function of both time and batch number. System monitoring must be sufficiently robust to adjust system operation to unexpected swings in process variables without risk of damage to the compressor and associated components.

Refrigerant selection is a function of the heat production profile and optimal production temperature of the medium to be cooled relative to the choice of cooling equipment. For example, in a batch style system with vacuum pump and ethanol refrigerant, it is difficult to maintain operating pressures below 0.15 psia (pounds per square inch absolute) due to the pressure drop between the vacuum source and the coil during system operation. However, 0.15 psia corresponds to an ethanol refrigerant vaporization temperature of approximately 40° F., thus the vacuum pump and ethanol refrigerant combination is best suited for those applications which maintain the medium to be cooled at or above 40° F. After installation, pressure drop between the vacuum source and the coil must again be calculated as a function of system geometry to ensure that the selected refrigerant will vaporize at the desired temperature to allow for successful system operation. Operationally, the refrigerant vapor pressure corresponds to the refrigerant vaporization temperature. The objective is to control the vapor pressure of the refrigerant in the coil at a specific vaporization temperature, at or near that of the set-point temperature of the medium to be cooled.

For fermentation of wine, common maximum allowable temperature ranges are 64-77° F. for red wines and 50-59° F. for whites. Assuming an ethanol refrigerant and vacuum pump combination, these temperature ranges correspond to vapor pressures of approximately 0.232-0.288 psia for red wines and 0.184-0.213 psia for white wines. Assuming an R-134a refrigerant and compressor combination, these temperature ranges correspond to vapor pressures of approximately 77.10-96.11 psia for red wines and 59.98-70.61 psia for white wines.

For fermentation of beer, common maximum allowable temperature ranges are 60-70° F. for ales and 45-55° F. for lagers. Assuming an ethanol refrigerant and vacuum pump combination, these temperature ranges correspond to vapor pressures of approximately 0.217-0.256 psia for ales and 0.169-0.200 psia for lagers. Assuming an R-134a refrigerant and compressor combination, these temperature ranges correspond to vapor pressures of approximately 71.87-85.48 psia for ales and 54.62-65.72 psia for lagers.

The system must also provide cooling for the duration of the fermentation cycle. For primary fermentation of both red and white wines, 3-5 days is commonly required. For primary fermentation of beer, 1-2 weeks is commonly required for ales and 1-2 months is commonly required for lagers.

It will be appreciated that the present disclosure can be implemented in various systems, apparatus, and devices for a number of applications. These include, without limitation:

1. Artificial generation of convective currents to promote thermosiphon agitation/homogenization of the medium via vaporizing refrigerant held at different pressures.

2. Use of vaporizing refrigerant to indicate the spatial location of heat transfer.

3. Use of a buffer cooling fluid to improve the consistency of heat transfer, where the buffer fluid is in thermal contact with both the refrigerant reservoir and the medium.

4. Generation of currents inside the vaporizing refrigerant to improve heat transfer by variation of vapor pressure.

5. Pre-heat of the refrigerant, before supply to the vaporization apparatus, to provide heating of the medium such that both heating and vaporization cooling can be affected by the same refrigerant vaporization apparatus.

Each of these implementations is described in more detail below and in connection with the accompanying figures.

1. Artificial Generation of Convective Currents to Promote Thermosiphon Agitation/Homogenization of the Medium Via Vaporizing Refrigerant Held at Different Pressures.

As shown in FIG. 11 , a system 120 is shown having multiple vertically arranged coil sections 122 within a container 124. The control of the different vertical coil sections 122 at different vacuum pressures is accomplished by using regulators 126 and pressure sensors (not shown), which may be manual or automatic, and which are coupled to a vacuum pump 128. They can be used to alter current flows inside the medium in the container 124, such as beer, improving heat transfer from the beer to the coil surface. They can also be used to control agitation of the beer through a thermo-siphon effect.

An electronic controller 130 that is coupled to the sensors, pressure regulators 126, and vacuum pump 128. The construction of the electronic controller 130 is within the ability of those of ordinary skill in this technology and will not be described in detail herein. Briefly, an on-site hard wired controller or a remote wireless controller, such as an app on a portable computing or portable communication device, such as a cell phone, tablet, and the like is provided to communicate with the components to monitor conditions and provide control signals thereto. Controlled agitation is important in fermentation, transfer, and storage and the pressures may be either fixed or cycled and automated control and maintenance of head space pressure for the cooling medium can be regulated. A single, pressure control set-point is possible for all reservoir head space via a pressure transmitter measuring head space pressure and electronic communication with the vacuum source. The reservoir head space may also be divided into sections, such that separate portions of the cooling medium reservoir can be controlled in different zones at differing pressures.

In accordance with one aspect, thermo-siphon agitation can be utilized for homogenization during fermentation and to maintain this homogenization during the lager aging phase (during and after the cold crash to near 32° F.). Thermo-siphon agitation may be optimized to control wort strong movement during fermentation, increasing the contact efficiency between yeast and wort.

The reservoir of the heat exchanger is in fluid communication with a cooling medium supply and vacuum source such that the cooling medium fills the reservoir leaving a selected amount of head space. The reservoir is also in fluid communication with the vacuum source for pulling a vacuum of a desired level in the reservoir head space, providing for a controlled vacuum vaporization at a low temperature at or near that of the medium (such as beer). Assuming an ethanol refrigerant, the vacuum level would be between 0.169 psi and 0.200 psi for lagers, equivalent to a fermentation temperature of 45° F.-55° F., and between 0.248 psi and 0.265 psi for ales, equivalent to a fermentation temperature of 68° F.-72° F. In addition, an indication of head space pressure can be provided such that vaporization of the cooling medium is detected and displayed, indicating thermal activity inside the medium.

In accordance with a further aspect of the present disclosure, a cooling coil is utilized for the interior bottom of the fermentation tank, replacing a second cooling jacket used for aging of lagers. This cooling coil improves homogenization by preventing beer separation due to gravity, density, or temperature differences, or any combination of the forgoing, when yeasts are predominately dormant or not producing the CO₂ required for natural agitation.

2. Use of Vaporizing Refrigerant to Indicate the Spatial Location of Heat Transfer.

In accordance with another aspect or implementation of the present disclosure, a temperature probe or site-glass, pressure, and vacuum gauge or other instrument is used to view or determine the vaporization rate of the fluid in the conduit. The vaporization rate is indicated by increased motion of the liquid refrigerant or by bubbles that form on the interior surface of the temperature control conduit or heat exchanger. These bubbles first form on the surface of the refrigerant reservoir, and then eventually detach and move upwards toward the head space. An operator, such as a brewer, can use the site-glasses or instruments to view the vaporization process and have visual or instrument-supplemented data to determine where heat is being generated by observing where the fluid motion occurs or where bubbles are being formed.

Some brewers turn off their cooling systems because they have no accurate way of protecting against local thermal spots only and do not want to risk thermal shock of the entire batch via activation of the cooling jacket. The present disclosure can also provide continued indication of local heat production through the unexpected presence of cooling medium downstream of the pump discharge. For example, indication may be used to signal the brewer to take corrective action to re-homogenize the tank.

3. Use of a Buffer Cooling Fluid to Improve the Consistency of Heat Transfer, where the Buffer Fluid is in Thermal Contact with Both the Refrigerant Reservoir and the Medium.

FIG. 12 shows a system 132 employing a coil or series of connected coils 134 mounted on the exterior 136 of a container 138, such as a jacketed fermenter tank. A medium 140 is contained within the container 138. In this implementation, the coils 134 attached to the exterior 136 of the container 138 provide contact between a fluid or buffer fluid in the coil and both the container 138 and the medium 140 in the container 138.

4. Generation of Currents Inside the Vaporizing Refrigerant to Improve Heat Transfer by Variation of Vapor Pressure.

In accordance with still yet a further aspect of the present disclosure, the cooling coil mechanical design provides for agitation of cooling fluid inside the cooling coil tubes themselves, further improving heat transfer from the cooling liquid in the coil to the vapor interface. Agitation results from the mechanical design, by which a common refrigerant vapor space is linked to at least two ends of a liquid refrigerant filled coil. As the liquid refrigerant vaporizes due to vacuum, the vapor generated moves toward the common vapor space, and this movement causes agitation of the refrigerant liquid volume between the vapor source and common headspace. However, because the liquid refrigerant volume is connected to a common headspace at more than one location, vapor generation causes part of the liquid volume to move in a direction opposite that of which the vapor is traveling, and this portion of liquid can move to fill part of the common headspace. The result is that part of the liquid refrigerant in the coil then moves relative to the coil interior surface. Liquid refrigerant movement promotes uptake of refrigerant vapor, generated on the interior surface of the coil, into the refrigerant liquid, and thereby improves heat transfer from the medium external to the coil to the refrigerant contained therein. For example, assuming an ethanol refrigerant, a vacuum level between 0.248 psi and 0.265 psi would be required, equivalent to a fermentation temperature of 68° F.-72° F. for beer ales.

The foregoing is illustrated in FIG. 13 , which shows a vacuum coil and reservoir system 142 consisting of two coils, a first coil 144 and a second coil 146, coupled to a common vacuum coil reservoir 148, at the top 150 of which is a vacuum equalization line 152. Each of the first and second coils 144, 146 have a first end 154, 156 respectively coupled to individual first and second ports 158, 160 at the empty head-space at the top 150 of the reservoir 148. In addition, each of the first and second coils 144, 146 have a second end 162, 164 respectively coupled to a common port 166 at the second end 168 or the liquid full part of the reservoir 148. Essentially, when vacuum is enabled, the liquid in the coils 144, 146 begins to oscillate relative to the two connection ports 158, 160 at the top 150 of the reservoir 148. When observed through clear coil tubing, it appears that the liquid tries to escape through one side of the top connection ports 158, 160, then gets dragged back and tries to escape then through the other side of the top connection, but is never successful in escaping through either connection. This would be the observed oscillatory motion. The reservoir is mechanically configured to replenish the liquid refrigerant vaporized, holding constant the level of the liquid refrigerant in the coil, relative to the starting and ending positions of the oscillations

5. Pre-Heating of the Refrigerant.

When refilling the system with refrigerant, the refrigerant can be heated above the current temperature of the medium. Once introduced to the refrigerant reservoirs, heat is conducted through the reservoir walls to the medium as the refrigerant cools, thus warming the medium. The refrigerant is then vaporized when cooling is desired. Thus, both heating and vaporization cooling can be affected by the same refrigerant vaporization apparatus.

The various implementations described above can be combined or revised to provide further implementations. For example, FIG. 14 illustrates an alternative implementation of the apparatus of FIG. 8 where refrigerant vapor streams are routed via vertical piping 170 to be brought together for collection above and outside the vessel or container. The diameter of the vertical piping 170 that routes the vapor streams can be smaller than the diameter of the horizontal tubes that form the respective reservoir sections 80, which increases the velocity of escaping refrigerant vapor streams. This helps to avoid condensation in the vertical piping 170, which would prevent vaporized refrigerant from escaping the cooling coil. In addition, there are fill and drain lines 171 that connect each manifold 112 to the common refrigerant fill and drain line 116. The orientation of the piping that forms the fill and drain lines 171 can be varied based upon the desired level of refrigerant 82 to be held in each manifold 112 after system drain.

FIG. 15 an alternative implementation of the apparatus of FIG. 8 that is suited for both a vacuum pump and traditional refrigerant compressor. Here, a refrigerant reservoir 172 is provided that includes a plurality of the reservoir sections 80 coupled in series by vertical risers 176 to form a continuous arrangement with an input port 174 at the top through which liquid refrigerant 82 enters. A combination drain and vacuum port 178 is provided at the other end, which allows for system drain as well as connection to the vacuum pump 92 or traditional refrigerant compressor. In this implementation, the liquid refrigerant 82 enters the input port 174 at the top of the system and vapor is removed from drain port 178 at the bottom. The vertical risers or tubing 176 can also be of a smaller diameter than the horizontal tubing of the reservoir sections 80 to promote vapor passage from horizontal tier to horizontal tier. This coil would be suitable to use for heating of a medium via circulation of warm refrigerant in either direction between the input port 174 and the drain port 178.

These and other changes can be made to the implementations in light of the above-detailed description. In general, in the following claims, the terms used should not be construed to limit the claims to the specific implementations disclosed in the specification and the claims, but should be construed to include all possible implementations along with the full scope of equivalents to which such claims are entitled. Accordingly, the claims are not limited by the disclosure. 

The invention claimed is:
 1. A system to control a temperature of a medium by refrigerant vaporization, comprising: a container having an exterior and an interior; at least one refrigerant reservoir associated with the container, the at least one refrigerant reservoir having at least one reservoir section configured to hold refrigerant, each at least one reservoir section having a wall with an exterior surface structured to be thermally coupled with a volume of the medium in the container and to provide thermal change to the volume of the medium in the container and thereby provide a volume of medium thermal coverage in the container, the volume of medium thermal coverage having an outside boundary; a vapor pressure apparatus to provide regulation of refrigerant vapor pressure in the at least one refrigerant reservoir; and wherein the at least one refrigerant reservoir is configured to form a vapor space in each of the at least one reservoir sections in response to receiving refrigerant and in response to the vapor pressure apparatus regulation of vapor pressure above the refrigerant to enable refrigerant vaporization at or near a selected temperature of the volume of medium thermal coverage for the volume of the medium in the container that is thermally coupled to the respective at least one reservoir section; and wherein the at least one reservoir section comprises a plurality of reservoir sections that each have a respective internal reservoir space that is in fluid communication with at least one other internal reservoir space of an adjacent reservoir section, and the plurality of reservoir sections are arranged in spaced relationship to adjacent reservoir sections with the respective volumes of medium thermal coverage having the respective boundaries of thermal coverage to be at least contiguous.
 2. The system of claim 1 further comprising a refrigerant source in fluid communication with the refrigerant reservoir and the vapor pressure apparatus and configured to provide refrigerant to the refrigerant reservoir in response to a change in vapor pressure in the refrigerant reservoir as regulated by the vapor pressure apparatus.
 3. The system of claim 1 wherein the plurality of reservoir sections are coupled together in series or in parallel or in a combination of series and parallel arrangements.
 4. The system of claim 1 wherein each internal reservoir space is formed by at least one weir in the respective reservoir section, with the at least one weir sized and shaped to divide the reservoir section into a vapor space and a refrigerant space.
 5. The system of claim 1 wherein the refrigerant reservoir comprises a lattice of reservoir sections.
 6. The system of claim 1 wherein the at least one refrigerant reservoir is located in the interior of the container.
 7. The system of claim 1 wherein the at least one refrigerant reservoir is located on the exterior of the container.
 8. The system of claim 1 in which R3 is a radius of the volume of medium thermal coverage that is determined as follows: ${R\; 3} = \sqrt{{\frac{1}{J*\pi}*\left( {{T\; 2} - {T\; 1}} \right)*\frac{1}{\frac{1}{2*\pi}*\left( {\frac{1}{H\; 1*R\; 1} + \frac{\ln\left( \frac{R\; 2}{R\; 1} \right)}{K\; 1} + \frac{1}{H\; 2*R\; 2}} \right)}} + {R\; 2^{2}}}$ where: H1=Refrigerant heat transfer coefficient, including boundary layer effects (W/m²*K); H2=Medium heat transfer coefficient, including boundary layer effects (W/m²*K); J=Heat generated by medium per unit volume per unit time (W/m³); K1=Thermal conductivity of refrigerant reservoir wall material of construction (W/m*K); R1=Radius from center of reservoir section to interior of reservoir section wall (m); R2=Radius from center of reservoir section to exterior of reservoir section wall (m); R3=Radius from center of reservoir section to outside boundary of medium thermal coverage (m); T1=Temperature of refrigerant at a location of vaporization (K); and T2=Temperature of the medium at an outer boundary of thermal coverage (K).
 9. The system of claim 8 wherein a minimum spacing between a center of adjacent reservoir sections is not less than $\frac{2}{\sqrt{2}}*R\; 3$ and in which R3 is a radius of the volume of medium thermal coverage. 